CN201241102Y - Naphtha fecundation aromatic hydrocarbons reforming system - Google Patents
Naphtha fecundation aromatic hydrocarbons reforming system Download PDFInfo
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- CN201241102Y CN201241102Y CNU2008201083730U CN200820108373U CN201241102Y CN 201241102 Y CN201241102 Y CN 201241102Y CN U2008201083730 U CNU2008201083730 U CN U2008201083730U CN 200820108373 U CN200820108373 U CN 200820108373U CN 201241102 Y CN201241102 Y CN 201241102Y
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Abstract
The utility model discloses a Naphtha prolific arene reforming system, and the system comprises a heating device and reaction devices; and is characterized in that: the reaction devices are connected with a high pressure separator; the high pressure separator is connected with a stabilization system; the lower part of the stabilization system is connected with an extraction system by a pipeline; the extraction system is connected with a raffinate oil cutting system by a pipeline on the one hand; the middle part of the raffinate oil cutting system is connected with the other reaction device by a pipeline and a heating device, the lower part of the raffinate oil cutting device extracts coal oil through the pipeline; and the other end of the other reaction device is connected with the high pressure separator by a pipeline. The utility model has the advantages of greatly increased processing capacity, liquid yield, arene yield and hydrogen output.
Description
Technical field
The utility model relates to a kind of The catalytic reforming system, particularly a kind of naphtha productive aromatic hydrocarbon reforming system.
Background technology
Along with rapid development of automobile industry and petrochemical industry to the aromatic hydrocarbons growth of requirement; particularly country is to the increasingly stringent requirement of environment protection, and catalytic reforming gasoline becomes one of ideal blend component in the New standard gasoline with its high-octane rating, low alkene and Trace Sulfur.For improving oil quality, the industry of development hydrogenation provides a large amount of cheap hydrogen sources to a large amount of hydrogen of catalytic reforming by product again.Therefore, catalytic reforming is being brought into play more and more important effect as the important oil refining process of producing stop bracket gasoline and aromatic hydrocarbons in oil refining, chemical engineering industry.
Catalytic reforming unit is pressed the catalyst regeneration mode, mainly can be divided into semi-regenerative reforming and CONTINUOUS REFORMER two classes at present.Two class catalytic reforming units are selected by its different raw material processing request by each refinery because of having different separately characteristics.
Semi-regenerative reforming is little owing to plant investment, flexible operation, and process cost is low, is suitable for different characteristics such as industrial scale, still takies critical role.
Since platinum/rhenium catalyst came out, the research of semi-regenerative reforming catalyzer and application had obtained sufficient development, have arrived quite high level.Half-regeneration reformer faces the pressure that enlarges processing power mostly, the capacity expansion revamping approach that yes deals with problems, but increase little device for load, if can be by improving catalyst activity, increasing the charging air speed, thereby improve unit capacity, then is best method.On the other hand, the reformer feed source presents diversified trend, and secondary processing oil such as the petroleum naphtha of low arene underwater content and coker gasoline proportion in reformer feed strengthens, and the poor quality trend of reformer feed is more and more obvious.The poor qualityization of raw material is had higher requirement to catalyst activity.
Therefore providing a kind of can improve processing power, and the naphtha productive aromatic hydrocarbon reforming system of raising liquid yield, aromatic production, octane value and hydrogen output just becomes the difficult problem that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides and a kind ofly can improve processing power, and improves the naphtha productive aromatic hydrocarbon reforming system that liquid yield, aromatic production and hydrogen yield provide the high-octane rating product simultaneously.
For achieving the above object, the utility model is taked following technical scheme:
A kind of naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit is divided into two portions, first and/or second reaction unit is connected with the diced system of raffinating oil by high-pressure separation apparatus, stabilizer tower system and extraction system, and the described diced system of raffinating oil is connected with the 3rd and/or the 4th reaction unit again.
A kind of optimal technical scheme is characterized in that: described reaction unit bottom is connected with high-pressure separator by pipeline; Described high-pressure separator is connected with stable system by pipeline, and is connected with the raw material supply system by pipeline and compression set; Described stable system bottom is connected with extraction system by pipeline; Described extraction system is connected with the diced system of raffinating oil by pipeline on the one hand; Described extraction system is on the other hand by pipeline extraction BTX aromatics; Raffinate oil by pipeline extraction lightweight in the described diced system top of raffinating oil, the described diced system middle part of raffinating oil is connected with another reaction unit (the 3rd reaction unit) by pipeline and heating unit, and the described cutting unit bottom of raffinating oil is by pipeline extraction kerosene; The other end of described another reaction unit is connected with described high-pressure separator with refrigerating unit by pipeline.
A kind of optimal technical scheme is characterized in that: described reaction unit is connected with second reaction unit by second heating unit.
A kind of optimal technical scheme is characterized in that: described another reaction unit is placed in-line two reactors up and down.
A kind of optimal technical scheme is characterized in that: described another reaction unit is connected with the 4th reaction unit by the 4th heating unit.
A kind of optimal technical scheme is characterized in that: described reaction unit is placed in-line two reactors up and down.
A kind of naphtha productive aromatic hydrocarbon reforming method, its step is as follows: boiling range is after 80-185 ℃ feed naphtha heats through heating unit, to enter reaction unit and react; The temperature in of described reaction unit is 470-530 ℃, and inlet pressure is 1.6-1.9MPa; Temperature out is 410-460 ℃, and top hole pressure is 1.5-1.8MPa; The gained reaction product is gone into high-pressure separator and is carried out high pressure and separate through overcooling is laggard, and the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After the high pressure separation, a gained hydrogen part is sent outside, and a part is back to feed line and another reaction unit through compression set; The gained reformate enters the stabilizer tower system and handles, and the tower top temperature of described stabilizer tower system is 100-120 ℃, and pressure is 0.8-1.05MPa, and column bottom temperature is 220-240 ℃, and pressure is 1.5-3.5MPa, and reflux ratio is 0.90-1.15; Cat head extraction liquefied gas; The gained boiling range is that 71-195 ℃ reformed oil enters extraction system and handles at the bottom of the tower, and the service temperature of described extraction system is 80-110 ℃, and working pressure is 0.6-0.8MPa, and solvent ratio is 2.5-3.5, returns and washes than being 0.4-0.6; Through after the extracting, the BTX aromatics extraction, all the other components enter the diced system cutting of raffinating oil through the top, the head temperature of described diced system is 58-86 ℃, and pressure is 0.1-0.3MPa, and bottom temp is 155-195 ℃, pressure is 0.15-0.34MPa, and reflux ratio is 20-60; Bottom extraction kerosene, top extraction lightweight is raffinated oil; Side line extraction mouth temperature is 100-140 ℃, and pressure is 0.12-0.25MPa, and the extraction treated oil reacts through entering another reaction unit after the heating, enters high-pressure separation apparatus after the cooling of gained reaction product.
A kind of optimal technical scheme is characterized in that: the reaction product of described reaction unit through after second heating unit heating, enters the reaction of second reaction unit again, and the gained reaction product enters high-pressure separation apparatus again after overcooling.
Extraction system described in the utility model is that the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation and water wash system.
The system of stabilizer tower described in the utility model and the diced system of raffinating oil comprise tower, air-cooler, watercooler, return tank, reflux pump and column bottoms pump etc. for conventional system.
Process furnace described in the utility model and condensing works are conventional device.
Catalyst system therefor described in the utility model in the reactor is conventional reforming catalyst.
Beneficial effect:
The advantage of naphtha productive aromatic hydrocarbon reforming system of the present utility model is: compare with existing catalytic reforming process, in the naphtha productive aromatic hydrocarbon reforming system of the present utility model, after the reacted product process extracting and the cutting of raffinating oil, the treated oil that generates with enter another reactor after recycle hydrogen mixes and further react, make the processing power of system of the present utility model improve, liquid yield, aromatic production and hydrogen yield improve greatly, and the high-octane rating product is provided simultaneously.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment 1.
Fig. 2 is the schematic flow sheet of the utility model embodiment 2.
Fig. 3 is the schematic flow sheet of the utility model embodiment 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment 1.Boiling range is 80-185 ℃, and sulphur content is 0.5ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 55% (m), and naphthene content is 35% (m), aromaticity content is 10% (m), and octane value (RON) is that 65,20 ℃ of density are 741 kilograms/meter
3Flow is 12.5 tons/hour feed purification petroleum naphtha process heat exchange earlier, after passing through process furnace 1-1 heating again, entering reactor 2-1 reacts, air speed is 3.0 than (air speed is than equaling the cumulative volume of feed purification petroleum naphtha divided by catalyzer), wherein reactor 2-1: reactor 2-2: reactor 2-3: reactor 2-4=1:1.5:2:3.5; The temperature in of described reactor 2-1 is 470 ℃, and inlet pressure is 1.6MPa (A); Temperature out is 410 ℃, and top hole pressure is 1.5MPa (A); The gained reaction product enters reactor 2-2 and reacts after heating through process furnace 1-2, and the temperature in of described reactor 2-2 is 470 ℃, and inlet pressure is 1.6MPa (A); Temperature out is 410 ℃, and top hole pressure is 1.5MPa (A); Enter high-pressure separator 4 and carry out the high pressure separation after heat exchange and condenser 3 coolings, the service temperature of described high-pressure separator 4 is 35 ℃, and working pressure is 1.2MPa (A); After the high pressure separation, a gained hydrogen part is sent outside, and its flow is 0.84 ton/hour, and hydrogen yield is 3.2% (weight); Other hydrogen is back to feed line and process furnace 1-3 through compressor 5, wherein being back to process furnace 1-1 preceding hydrogen to oil volume ratio is 800:1, entering process furnace 1-3 preceding hydrogen to oil volume ratio is 1200:1 (carrying out heat exchange before entering process furnace earlier), the temperature in of described reactor 2-3 is 470 ℃, and inlet pressure is 1.6MPa (A); Temperature out is 410 ℃, and top hole pressure is 1.5MPa (A); Enter stabilizer tower system 6 through high-pressure separator 4 gained reformates and handle, the tower top temperature of described stabilizer tower system 6 is 100 ℃, and pressure is 0.8MPa (A), and column bottom temperature is 220 ℃, and pressure is 1.5-3.5MPa (A), and reflux ratio (m/m) is 0.90; Cat head extraction liquefied gas and less water, its flow are 0.31 ton/hour; Gained reformed oil at the bottom of the tower (boiling range is 71-192 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 80 ℃, and working pressure is 0.6MPa (A), and solvent ratio is 2.5, returns and washes than being 0.4, and solvent for use is a tetramethylene sulfone; Through after the extracting, the BTX aromatics extraction, the boiling range of gained BTX aromatics is 102-192 ℃, sulphur content trace (can not detecting), alkane content are 0.16% (m), and naphthene content is 1.97% (m), aromaticity content is 98% (m), and octane value (RON) is that 118,20 ℃ of density are 851 kilograms/meter
3, flow is 9.7 tons/hour, aromatics yield is 76.05% (weight); Gained is raffinated oil and is entered the diced system 7 of raffinating oil through the top and carry out cutting and separating, and the head temperature of described diced system 7 is 58 ℃, and pressure is 0.1MPa (A), and bottom temp is 155 ℃, and pressure is 0.15MPa (A), and reflux ratio (m/m) is 20; Bottom extraction kerosene, the boiling range of gained kerosene is 147-185 ℃, sulphur content trace (can not detecting), alkane content is 96% (m), and naphthene content is 1.84% (m), and aromaticity content is 3.67% (m), octane value (RON) is that 44,20 ℃ of density are 796 kilograms/meter
3, flow is 1.25 tons/hour; Top extraction lightweight is raffinated oil, and the boiling range that the gained lightweight is raffinated oil is 71-80 ℃, sulphur content trace (can not detecting), alkane content is 75% (m), and naphthene content is 24% (m), and aromaticity content is 0.12% (m), octane value (RON) is that 77,20 ℃ of density are 685 kilograms/meter
3, flow is 0.4 ton/hour; Total liquid yield is 90.8%.Side line extraction mouth temperature is 100 ℃, pressure is 0.12MPa (A), extraction treated oil (three anti-chargings), the boiling range of gained treated oil is 80-147 ℃, and sulphur content trace (can not detecting), alkane content are 92% (m), naphthene content is 6.72% (m), aromaticity content is 1.35% (m), and octane value (RON) is that 55,20 ℃ of density are 721 kilograms/meter
3, flow is 9 tons/hour; React through entering reactor 2-3 after the heating, the gained reaction product enters reactor 2-4 reactions after process furnace 1-4 heating, and the temperature in of described reactor 2-4 is 470 ℃, and inlet pressure is 1.6MPa (A); Temperature out is 410 ℃, and top hole pressure is 1.5MPa (A); The gained reaction product with after the reaction product of described reactor 2-2 is mixed through entering high-pressure separator 4 after heat exchange and condenser 3 coolings.
The used reforming catalyst of the utility model is a kind of Pt, Re reforming catalyst, its carrier mixes by a certain percentage for single diaspore of GM and the single diaspore of Ziegler synthesising by-product SB that adopts aluminium colloidal sol deep fat ageing process and make, the compound γ-aluminium sesquioxide that two concentrated Kong Feng are arranged that makes through moulding, roasting.Pt content is 0.10～1.00 heavy % on the catalyzer, and Re content is 0.10～3.00 heavy %, and Cl content is 0.50～3.00 heavy %, and this catalyzer has the characteristics of high reactivity, highly selective and low carbon deposit.
Total liquid yield equals flow sum that BTX aromatics, kerosene and lightweight raffinate oil divided by the raw material inlet amount in the utility model.
Aromatics yield equals the BTX aromatics flow and multiply by aromaticity content again divided by the raw material inlet amount.
Hydrogen yield equals to efflux the hydrogen amount and multiply by hydrogen purity again divided by the raw material inlet amount.
The physico-chemical property of reactor 2-1 and 2-2 catalyst system therefors is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 192 | 183 | 0.52 | 0.75 | 0.25 | 0.25 |
The physico-chemical property of reactor 2-3 and 2-4 catalyst system therefors is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 196 | 187 | 0.54 | 0.74 | 0.26 | 0.45 |
The used measuring method of the utility model is (down together):
1, boiling range: GB/T6536-1997 measured for petroleum product distillation method;
2, sulphur content: the total sulfur content assay method (ultraviolet fluorescence method) of SH/T0689-2000 light hydrocarbon and motor spirit and other oil products;
3, mercaptan sulfur: mercaptan sulfur assay method (potentiometric titration) in the GB/T1792-1988 distillate fuel oil;
4, alkane: SH/T0239-92 thin layer packed column chromatography;
5, aromatic hydrocarbons: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
6, octane value: GB/T5487 testing octane number of gasoline method (organon);
7, density: GB/T1884-2000 crude oil and liquid petroleum product density experiment chamber assay method (densimeter method);
8, naphthenic hydrocarbon: SH/T0239-92 thin layer packed column chromatography;
9, metal in the oil: the standard test methods of nickel, vanadium and iron in ASTM D 5708-2005 inductively coupled plasma (ICP) aes determination crude oil and the trapped fuel;
10, nitrogen content: the SH/T0704-2001 chemoluminescence method is surveyed nitrogen (boat sample introduction).
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the utility model embodiment 2.Boiling range is 80-185 ℃, and sulphur content is 0.54ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 54% (m), and naphthene content is 36% (m), aromaticity content is 11% (m), and octane value (RON) is that 68,20 ℃ of density are 743 kilograms/meter
3, flow be 12.5 tons/hour feed purification petroleum naphtha earlier through heat exchange, pass through process furnace 1-1 heating again after, enter reactor 2-1 and react; Air speed (air speed equals the cumulative volume of feed purification petroleum naphtha divided by catalyzer) is 3.0, wherein on the reactor 2-1: reactor 2-1 time: on the reactor 2-2: 2-2 times=1:1.5:2:3.5 of reactor; The temperature in of described reactor 2-1 is 480 ℃, and inlet pressure is 1.8MPa (A); Temperature out is 430 ℃, and top hole pressure is 1.7MPa (A); Wherein said reactor 2-1 is that placed in-line up and down two reactors are formed, be provided with process furnace 1-2 between two reactors, after heat exchange and condenser 3 coolings, enter high-pressure separator 4 through reactor 2-1 reaction back products therefrom and carry out the high pressure separation, the service temperature of described high-pressure separator 4 is 40 ℃, and working pressure is 1.3MPa (A); After the high pressure separation, a gained hydrogen part is sent outside, and its flow is 0.83 ton/hour, and hydrogen yield is 3.2% (weight); Other hydrogen is back to feed line and well heater 1-3 through compressor 5, wherein being back to process furnace 1-1 preceding hydrogen to oil volume ratio is 800:1, entering process furnace 1-3 preceding hydrogen to oil volume ratio is 1200:1 (carrying out heat exchange before entering process furnace earlier), the temperature in of described reactor 2-2 is 480 ℃, inlet pressure is 1.4-1.7MPa (A), preferred 1.6MPa (A); Temperature out is 430 ℃, and top hole pressure is 1.3-1.6MPa (A), preferred 1.5MPa (A); Enter stabilizer tower system 6 through high-pressure separator 4 gained reformates and handle, the tower top temperature of described stabilizer tower system 6 is 102 ℃, and pressure is 0.95MPa (A), and column bottom temperature is 227.5 ℃, and pressure is 2.5MPa (A), and reflux ratio (m/m) is 0.99; Cat head extraction liquefied gas and less water, its flow are 0.32 ton/hour; Gained reformed oil at the bottom of the tower (boiling range is 71-193 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 90 ℃, and working pressure is 0.7MPa (A), and solvent ratio is 3, returns and washes than being 0.45, and solvent for use is a tetramethylene sulfone; Through after the extracting, the BTX aromatics extraction, the boiling range of gained BTX aromatics is 102-193 ℃, sulphur content trace (can not detecting), alkane content are 0.16% (m), and naphthene content is 1.97% (m), aromaticity content is 98% (m), and octane value (RON) is that 118,20 ℃ of density are 851 kilograms/meter
3, flow is 9.67 tons/hour, aromatics yield is 75.81% (weight); Gained is raffinated oil and is entered the diced system 7 of raffinating oil through the top and carry out cutting and separating, and the head temperature of described diced system 7 is 59 ℃, and pressure is 0.1MPa (A), and bottom temp is 158 ℃, and pressure is 0.16MPa (A), and reflux ratio (m/m) is 30; Bottom extraction kerosene, the boiling range of gained kerosene is 147-185 ℃, sulphur content trace (can not detecting), alkane content is 95% (m), and naphthene content is 1.83% (m), and aromaticity content is 3.59% (m), octane value (RON) is that 44,20 ℃ of density are 795 kilograms/meter
3, flow is 1.28 tons/hour; Top extraction lightweight is raffinated oil, and the boiling range that the gained lightweight is raffinated oil is 71-80 ℃, sulphur content trace (can not detecting), alkane content is 73% (m), and naphthene content is 23% (m), and aromaticity content is 0.12% (m), octane value (RON) is that 77,20 ℃ of density are 685 kilograms/meter
3, flow is 0.4 ton/hour; Total liquid yield is 90.8% (weight).Side line extraction mouth temperature is 120 ℃, pressure is 0.19MPa (A), extraction treated oil (three anti-chargings), the boiling range of gained treated oil is 80-147 ℃, sulphur content trace (can not detecting), alkane content is 92% (m), naphthene content is 6.72% (m), and aromaticity content is 1.35% (m), and octane value (RON) is 55,20 ℃ of density is 720 kilograms/meter 3, and flow is 8.8 tons/hour; The gained treated oil enters reactor 2-2 after through process furnace 1-3 heating and reacts, and described reactor 2-2 be placed in-line two reactors composition of up-down structure, between be provided with process furnace 1-4; Enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
The physico-chemical property of reactor 2-1 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 192 | 183 | 0.52 | 0.75 | 0.25 | 0.25 |
The physico-chemical property of reactor 2-2 catalyst system therefors is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 196 | 187 | 0.54 | 0.74 | 0.26 | 0.45 |
As shown in Figure 3, be the schematic flow sheet of the utility model embodiment 3.Boiling range is 80-185 ℃, and sulphur content is 0.45ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 54% (m), and naphthene content is 33% (m), aromaticity content is 12% (m), and octane value (RON) is that 67,20 ℃ of density are 743 kilograms/meter
3, flow be 12.5 tons/hour refining petroleum naphtha earlier through heat exchange, pass through process furnace 1-1 heating again after, enter reactor 2-1 and react; Air speed (air speed equals the cumulative volume of feed purification petroleum naphtha divided by catalyzer) is 3.0, wherein reactor 2-1: reactor 2-2=1:2; The temperature in of described reactor 2-1 is 530 ℃, and inlet pressure is 1.9MPa (A); Temperature out is 460 ℃, and top hole pressure is 1.8MPa (A); The gained reaction product enters high-pressure separator 4 and carries out the high pressure separation after heat exchange and condenser 3 coolings, the service temperature of described high-pressure separator 4 is 45 ℃, and working pressure is 1.4MPa (A); After the high pressure separation, a gained hydrogen part is sent outside, and its flow is 0.9 ton/hour, and pure hydrogen flow is 0.325% (weight), and hydrogen yield is 3.0% (weight); Other hydrogen is back to feed line and process furnace 1-2 through compressor 5, wherein being back to process furnace 1-1 preceding hydrogen to oil volume ratio is 800:1, entering process furnace 1-2 preceding hydrogen to oil volume ratio is 1200:1 (carrying out heat exchange before entering process furnace earlier), the temperature in of described reactor 2-2 is 530 ℃, and inlet pressure is 1.9MPa (A); Temperature out is 460 ℃, and top hole pressure is 1.8MPa (A); Enter stabilizer tower system 6 through high-pressure separator 4 gained reformates and handle, the tower top temperature of described stabilizer tower system 6 is 120 ℃, and pressure is 1.05MPa (A), and column bottom temperature is 240 ℃, and pressure is 3.5MPa (A), and reflux ratio (m/m) is 1.15; Cat head extraction liquefied gas and less water, its flow are 0.33 ton/hour; Gained reformed oil at the bottom of the tower (boiling range is 71-195 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 110 ℃, and working pressure is 0.8MPa (A), and solvent ratio is 3.5, returns and washes than being 0.6, and solvent for use is a tetramethylene sulfone; Through after the extracting, the BTX aromatics extraction, the boiling range of gained BTX aromatics is 101-195 ℃, sulphur content trace (can not detecting), alkane content are 0.15% (m), and naphthene content is 1.96% (m), aromaticity content is 98% (m), and octane value (RON) is that 119,20 ℃ of density are 851 kilograms/meter
3, flow is 9.2 tons/hour, aromatics yield is 76.05% (weight); Gained is raffinated oil and is entered the diced system 7 of raffinating oil through the top and carry out cutting and separating, and the head temperature of described diced system 7 is 86 ℃, and pressure is 0.3MPa (A), and bottom temp is 188 ℃, and pressure is 0.34MPa (A), and reflux ratio (m/m) is 60; Bottom extraction kerosene, the boiling range of gained kerosene is 146-186 ℃, sulphur content trace (can not detecting), alkane content is 95% (m), and naphthene content is 1.85% (m), and aromaticity content is 3.32% (m), octane value (RON) is that 45,20 ℃ of density are 795 kilograms/meter
3, flow is 1.59 tons/hour; Top extraction lightweight is raffinated oil, the boiling range that the gained lightweight is raffinated oil is 71-80 ℃, sulphur content trace (can not detecting), alkane content is 76% (m), naphthene content is 23% (m), and aromaticity content is 0.12% (m), and octane value (RON) is 77,20 ℃ of density is 685 kilograms/meter 3, and flow is 0.48 ton/hour; Total liquid yield is 90.16% (weight).Side line extraction mouth temperature is 140 ℃, pressure is 0.25MPa (A), extraction treated oil (three anti-chargings), the boiling range of gained treated oil is 80-147 ℃, and sulphur content trace (can not detecting), alkane content are 93% (m), naphthene content is 6.70% (m), aromaticity content is 1.35% (m), and octane value (RON) is 55, is 722 kilograms/meter 20 ℃ of density
3, flow is 9.2 tons/hour; React through entering reactor 2-2 after process furnace 1-2 heating, enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
The physico-chemical property of reactor 2-1 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 192 | 183 | 0.52 | 0.75 | 0.25 | 0.25 |
The physico-chemical property of reactor 2-2 catalyst system therefors is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 196 | 187 | 0.54 | 0.74 | 0.26 | 0.45 |
Claims (6)
1, a kind of naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit is divided into two portions, first and/or second reaction unit is connected with the diced system of raffinating oil by high-pressure separation apparatus, stabilizer tower system and extraction system, and the described diced system of raffinating oil is connected with the 3rd and/or the 4th reaction unit again.
2, a kind of naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit bottom is connected with high-pressure separator by pipeline; Described high-pressure separator is connected with stable system by pipeline, and is connected with the raw material supply system by pipeline and compression set; Described stable system bottom is connected with extraction system by pipeline; Described extraction system is connected with the diced system of raffinating oil by pipeline on the one hand; Described extraction system is on the other hand by the direct extraction BTX aromatics of pipeline; Raffinate oil by pipeline extraction lightweight in the described diced system top of raffinating oil, the described diced system middle part of raffinating oil is connected with another reaction unit by pipeline and heating unit, and the described cutting unit bottom of raffinating oil is by the direct extraction kerosene of pipeline; The other end of described another reaction unit is connected with described high-pressure separator with refrigerating unit by pipeline.
3, naphtha productive aromatic hydrocarbon reforming system according to claim 2 is characterized in that: described reaction unit is connected with second reaction unit by second heating unit.
4, naphtha productive aromatic hydrocarbon reforming system according to claim 3 is characterized in that: described another reaction unit is connected with the 4th reaction unit by the 4th heating unit.
5, according to claim 3 or 4 described naphtha productive aromatic hydrocarbon reforming systems, it is characterized in that: described another reaction unit is placed in-line two reactors up and down.
6, naphtha productive aromatic hydrocarbon reforming system according to claim 5 is characterized in that: described reaction unit is placed in-line two reactors up and down.
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| CNU2008201083730U CN201241102Y (en) | 2008-06-04 | 2008-06-04 | Naphtha fecundation aromatic hydrocarbons reforming system |
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| CNU2008201083730U CN201241102Y (en) | 2008-06-04 | 2008-06-04 | Naphtha fecundation aromatic hydrocarbons reforming system |
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| CNU2008201083730U Expired - Lifetime CN201241102Y (en) | 2008-06-04 | 2008-06-04 | Naphtha fecundation aromatic hydrocarbons reforming system |
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